US7048772B1 - Secondary reforming process and burner - Google Patents

Secondary reforming process and burner Download PDF

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US7048772B1
US7048772B1 US09/913,314 US91331401A US7048772B1 US 7048772 B1 US7048772 B1 US 7048772B1 US 91331401 A US91331401 A US 91331401A US 7048772 B1 US7048772 B1 US 7048772B1
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gas flow
combustion chamber
oxygen
nozzles
burner
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Gianfranco Bedetti
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Casale SA
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Casale Chemicals SA
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/36—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents
    • C01B3/363—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents characterised by the burner used
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0278—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0285—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/38—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
    • C01B3/382—Multi-step processes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/20—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone
    • F23D14/22—Non-premix gas burners, i.e. in which gaseous fuel is mixed with combustion air on arrival at the combustion zone with separate air and gas feed ducts, e.g. with ducts running parallel or crossing each other
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/32—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid using a mixture of gaseous fuel and pure oxygen or oxygen-enriched air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/46—Details, e.g. noise reduction means
    • F23D14/48—Nozzles
    • F23D14/56—Nozzles for spreading the flame over an area, e.g. for desurfacing of solid material, for surface hardening, or for heating workpieces
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23D—BURNERS
    • F23D14/00—Burners for combustion of a gas, e.g. of a gas stored under pressure as a liquid
    • F23D14/46—Details, e.g. noise reduction means
    • F23D14/48—Nozzles
    • F23D14/58—Nozzles characterised by the shape or arrangement of the outlet or outlets from the nozzle, e.g. of annular configuration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00477—Controlling the temperature by thermal insulation means
    • B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00504—Controlling the temperature by means of a burner
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
    • C01B2203/0244—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being an autothermal reforming step, e.g. secondary reforming processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0816—Heating by flames
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0811—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel
    • C01B2203/0822—Methods of heating the process for making hydrogen or synthesis gas by combustion of fuel the fuel containing hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0838—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel
    • C01B2203/0844—Methods of heating the process for making hydrogen or synthesis gas by heat exchange with exothermic reactions, other than by combustion of fuel the non-combustive exothermic reaction being another reforming reaction as defined in groups C01B2203/02 - C01B2203/0294
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C01B2203/0866—Methods of heating the process for making hydrogen or synthesis gas by combination of different heating methods
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1005—Arrangement or shape of catalyst
    • C01B2203/1011—Packed bed of catalytic structures, e.g. particles, packing elements
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1276—Mixing of different feed components
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/142—At least two reforming, decomposition or partial oxidation steps in series
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/80—Aspect of integrated processes for the production of hydrogen or synthesis gas not covered by groups C01B2203/02 - C01B2203/1695
    • C01B2203/82—Several process steps of C01B2203/02 - C01B2203/08 integrated into a single apparatus
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the present invention relates to a process for carrying out secondary reforming reactions for the production of gas mixtures containing hydrogen and carbon monoxide, such as for example the synthesis gases for ammonia and methanol.
  • the present invention focuses on the exothermic combustion reaction that precedes the strongly endothermic steam reforming catalytic reaction.
  • the present invention concerns a process for secondary reforming comprising the steps of:
  • gas flow comprising oxygen is used to generically indicate a comburent gas comprising in addition to oxygen also steam and in case nitrogen; instead, the term: “gas flow comprising hydrocarbons”, is used for indicating a combustible or process gas comprising hydrogen, carbon monoxide, carbon dioxide and steam beside light hydrocarbons (for example C1–C4).
  • the combustible gas generally derives from a section of primary reforming wherein hydrocarbons like for example natural gas, naphtha, LPG (liquefied petroleum gas) or refinery gas, and mixtures thereof, are reacted with water steam. In the field these gases are also called transformed or reformed gases.
  • hydrocarbons like for example natural gas, naphtha, LPG (liquefied petroleum gas) or refinery gas, and mixtures thereof.
  • gas flow comprising hydrogen and carbon monoxide is used for indicating a gas flow comprising also N 2 , Ar and He beside CO and H 2 .
  • the invention also relates to a burner for carrying out the above-mentioned process.
  • the oxygen flow fed to the combustion chamber is split in a plurality of jets that depart radially in rows generally laid the one upon the other from a circular collector, whereas the hydrocarbons flow is made flow through these jets.
  • a plurality of radial flames are formed (a respective one for each jet), that are generally distributed in circular rows laid the one upon the other with respect to the direction of the process gas flow, and hence the combustion of a remarkable amount of process gas may take place even in a reduced space such as that of the combustion chamber.
  • the combustion chamber wherein the combustion of the hydrocarbons takes place is provided in the space defined above a catalytic bed for the next steam reforming reaction of the burnt gas comprising carbon monoxide and hydrogen.
  • the plurality of radial jets distributed in circular rows laid the one upon the other with respect to the flow direction of the hydrocarbons, is the main cause of a non optimal mixing of the reagent gases, also with the burnt gas, in the combustion chamber. This has the consequence of a non-homogeneous combustion, which worsen the yield of the subsequent steam reforming reaction to the detriment of the synthesis gas production.
  • This drawback is mainly due to the non-optimal positioning and dimensioning of the oxygen jets that thus intake different quantities of process gas, and burnt gas, with the subsequent formation of different flames, i.e. at different temperature and composition conditions.
  • this phenomenon may be further emphasised in the processes according to the prior art by a non-uniform flow rate of the gas flow comprising hydrocarbons which is fed in the combustion chamber near the oxygen jets.
  • the length of the flames is a critical parameter for an optimal exploitation of the combustion chamber. Too long flames may lap onto the lining of refractory material of the combustion chamber as well as onto the underlying catalyst, thus damaging both.
  • High pressure drop of the oxygen flow that, beside being used as comburent in the combustion reaction, is very important as coolant of the walls of the burner intended for carrying out the combustion reaction, with the purpose of avoiding damages or rapid deterioration thereof.
  • the comburent gas is made flow along specific paths in order to realise the aforesaid cooling with the consequence, however, of a high pressure drop of such flow, with negative consequences in terms of energy consumption and operating costs.
  • the technical problem at the basis of the present invention is that of providing a process for carrying out secondary reforming reactions, with a high yield, which is easy to carry out and does not require high operating and maintenance costs.
  • the aforesaid problem is solved by a process of the above indicated type, which is characterized in that it comprises the further steps of:
  • the present invention allows to optimise the combustion reaction of the hydrocarbons, and therefore to facilitate the production of synthesis gas, minimising the energy consumption and the operating and maintenance costs.
  • the gas flow comprising oxygen fed into the combustion chamber is split in a plurality of jets not laid the one upon the other in the direction of the gas flow comprising hydrocarbons.
  • each portion of flow comprising hydrocarbons directed into the combustion chamber contacts only one jet of oxygen and not a plurality of jets as is generally the case in the processes according to the prior art.
  • jets are split within the hydrocarbon gaseous flow so as to mix the gaseous flow comprising oxygen with amounts of gaseous flow comprising hydrocarbon in local constant ratio.
  • the end portion of the feeding duct which is in contact with the hot burnt gases and hence in general subjected to a rapid deterioration, can be cooled effectively and uniformly by all the oxygen flow rate, that is by a constant and homogeneous amount of oxygen that flows inside it.
  • the feeding duct of the burner for the combustion of the process gas
  • the gas flow comprising oxygen crosses the gas flow comprising hydrocarbons within the combustion chamber with a substantially transversal motion.
  • the energy consumption is further reduced subjecting the gas flow comprising oxygen passing through the feeding duct to an overall pressure drop comprised between 0,25 and 0,35 bar.
  • the jets of the gas flow comprising oxygen are fed into the combustion chamber with substantial orthogonal motion with respect to the direction of such flow inside the feeding duct.
  • a burner is also provided for secondary reforming of the type comprising:
  • FIG. 1 shows a schematic view in longitudinal section of a secondary reforming apparatus for the production of synthesis gas comprising a burner unit operating with the process according to a preferred embodiment of the present invention
  • FIG. 2 shows a schematic view in cross section of the burner unit shown in FIG. 1 , according to a preferred embodiment of the present invention
  • FIG. 3 shows a schematic view in longitudinal section of the burner unit of FIG. 2 , taken along line X—X;
  • FIG. 4 shows a schematic view in longitudinal section of a detail of the burner unit of FIG. 3 , taken along line Y—Y.
  • a secondary reforming apparatus of the type comprising a substantially cylindrical shell 2 wherein a catalyst bed 3 is arranged for carrying out reactions such as the steam reforming reaction for the production of synthesis gas.
  • a combustion chamber 4 for the combustion of the hydrocarbons and a chamber 5 for collecting the synthesis gas produced in the catalytic bed 3 , respectively.
  • combustion chamber 4 wherein the combustion reaction between the oxygen and the hydrocarbons takes place is delimited below by the maximum level reached by the catalyst inside the shell 2 , indicated in FIG. 1 by the dashed line 3 a , and above by a burner 6 that will be described hereinbelow in greater detail.
  • the inside of the shell 2 is lined with refractory material—indicated in general with 7 in FIG. 1 —resistant to high temperatures, as protection for the metallic structure of the shell.
  • the gas flow comprising hydrocarbons coming in general from the primary reforming section is introduced into the apparatus 1 through the gas inlet nozzle 8 .
  • the gas flow comprising oxygen is instead introduced into the apparatus 1 through the nozzle gas inlet 9 .
  • This flow called also comburent gas comprises in general air or air enriched in oxygen.
  • air enriched in oxygen is meant to indicate air with an oxygen content higher than 21% molar, for example comprised between 22% and 80%.
  • the synthesis gas resulting from the steam reforming catalytic reaction exits the apparatus 1 through the gas outlet nozzle 10 in fluid communication with the chamber 5 .
  • the secondary reforming apparatus 1 of FIG. 1 generally operates at temperatures comprised between 800–1000° C., and pressures comprised between 20–40 bar. In the field, this apparatus is also called autothermal reforming apparatus.
  • the materials and the catalyst used in secondary reformer apparatus 1 are of conventional type and will not be described in greater detail in the following description.
  • the burner 6 in FIG. 1 is housed in an upper appendix 2 a of the shell 2 of a smaller diameter than the latter.
  • first duct 12 substantially cylindrical and of predetermined length, which is in fluid communication with the inlet nozzle 9 for feeding the gas flow comprising oxygen to the underlying combustion chamber 4 .
  • a second duct 13 external and coaxial with respect to the burner 6 , provided in the appendix 2 a of the shell 2 , defines inside it—between the ducts 12 and 13 —a substantially annular hollow space 14 for feeding the gas flow comprising hydrocarbons to the combustion chamber 4 .
  • the hollow space 14 is in fluid communication with the inlet nozzle 8 that leads into the second duct 13 in orthogonal direction thereto.
  • the burner 6 according to the present invention further comprises at least one collector 15 for the gas flow comprising oxygen in fluid communication with an end 12 a of the first duct 12 .
  • the burner 6 comprises a plurality of collectors 15 that extend radially from the end 12 a of the first duct 12 .
  • the number of collectors 15 can vary from 4 to 12, according to the flow rate of the reactant gases and to the space available in the combustion chamber 4 .
  • the burner 6 comprises eight collectors 15 that extend radially along the circumference of the first duct 12 and at the same distance with respect to each other.
  • the collectors 15 comprise in turn a plurality of nozzles 16 distributed along the circumference of the collectors 15 near to a lower end 15 a thereof and arranged so as not to lay one upon the other with respect to the direction orthogonal to the end 15 a of collectors 15 .
  • the nozzles 16 are distributed along opposite walls 17 of the collectors 15 .
  • FIGS. 2–4 the details of the burner 6 equivalent for structure and operation to those illustrated in FIG. 1 will be indicated with the same reference numerals and will not be described again.
  • each portion of the burnt gas flowing near the burner 7 is entrained by only one jet of comburent gas.
  • the burner 6 according to the present invention permits therefore to obtain almost constant mixing conditions at the collectors 15 , which means working with flames all equal to each other and operating at the same temperature and composition conditions.
  • collectors 15 permits to have a great number of nozzles 16 of little diameter not laid the one upon the other with respect to the direction orthogonal to the end 15 a of collectors 15 . It follows that is possible to obtain a number of flames (one for each oxygen jet) such to enable the completion of the combustion reaction inside the combustion chamber 4 . At the same time, these flames are short enough to avoid any damage of the catalyst below the combustion chamber 4 or of the inner walls of this chamber.
  • the nozzles 16 are of circular shape. It is however possible to manufacture the nozzles 16 with different shape, for instance of substantially rectangular shape so as to obtain a plurality of adjacent slots.
  • the nozzles 16 are advantageously disposed along the perimeter of the collectors 15 at changing distance so as to maintain a constant mixing ratio between the gaseous flow comprising oxygen and the gaseous flow comprising hydrocarbons in each zone of the combustion chamber 4 facing the burner 6 .
  • a constant mixing ratio between the gaseous flow comprising oxygen and the gaseous flow comprising hydrocarbons in each zone of the combustion chamber 4 facing the burner 6 .
  • the radius Ri is equal to the distance between the axis A of the duct 12 and the nozzles 16 arranged on the i-th circumference.
  • Analogous criteria may be used in case of non-circular nozzles 16 .
  • the nozzles 16 can be suitably spaced apart so to ensure an optimal combustion in the chamber 4 and—among others—avoid undesired intersections or disturbances between adjacent jets, i.e. adjacent flames.
  • the distance of the latter along the collectors 15 results to be more and more close as the distance from the axis A of the conduct 12 increase.
  • homogeneous combustion conditions may also be obtained providing the nozzles 16 of varying size arranged along the perimeter of the collectors 15 at constant distance.
  • the nozzles 16 have a diameter comprised between 2 and 30 mm, preferably between 5 and 25 mm and even preferably between 5 and 15 mm.
  • the above mentioned dimensions of the nozzles 16 are particularly advantageous in that they allow to optimise the number and diameter of the nozzles that may be manufactured in the walls 17 of the collectors 15 .
  • the circular nozzles 16 are flared (countersunk) at an inner side 17 ′ of the walls 17 , as shown in FIG. 4 .
  • Such flaring is further advantageous in that it promotes an essentially laminar flow of the comburent gas through the nozzles 16 .
  • the lower end 15 a of the collectors 15 has preferably a substantially semicircular section for making the outflow of the gaseous flow comprising oxygen from the nozzles 16 easier, further minimising the pressure drop of such flow.
  • suitable means are advantageously provided for rendering the flow rate of the gaseous flow comprising hydrocarbons coming out from the substantially annular hollow space 14 uniform.
  • the means for rendering uniform the process gas flow rate comprises a plurality of perforated baffle plates 20 extending in the hollow space 14 nearby the collectors 15 . More exactly, the baffle plates 20 extend perpendicular to the walls 17 and parallel to the respective lower end 15 a of the collectors 15 , in a position just above the nozzles 16 .
  • baffle plate 20 it is also possible to provide only one baffle plate 20 depending upon the number and the shape of collectors 15 .
  • the inlet nozzle 8 of the process gas being in general perpendicular to the hollow space 4 defined between the ducts 12 and 13 , turbulence is formed in the gaseous flow comprising hydrocarbons flowing inside the hollow space 4 . This turbulence causes the flow rate of the flow fed to the combustion chamber 4 to be not uniform.
  • the amount of process gas entrained by any single oxygen jet coming out from the nozzles 16 is maintained constant and homogeneous in the proximity of the entire burner 6 , further promoting a correct and complete combustion of hydrocarbons.
  • the gaseous flow comprising hydrocarbons fed to the combustion chamber 4 is advantageously subjected to a predetermined pressure drop when leaving the substantial annular passage defined by the hollow space 14 , so as to uniform the flow rate of such flow.
  • the opposite walls 17 of the collectors 15 are advantageously plane and substantially parallel to each other. Further on, such walls 17 extend from the end 12 a of the first duct 12 with an angle preferably comprised between 30 and 60° with respect to the axis A of the duct 12 .
  • the collectors 15 have a substantially parallelepiped shape in such a way to promote a passage of the comburent gas through the collectors 15 as laminar as possible and with minor pressure drops.
  • the specific angular orientation of the collectors 15 with respect to the axis A of the first duct 12 permits to confine the mixing zone of the gaseous reactants near an upper end of the combustion chamber 4 so to exploit at most the available space for the combustion reaction.
  • the lower end 15 a of the collectors 15 is advantageously rectilinear and is provided with a tilt angle comprised between 45° and 90° with respect to axis A, preferably between 60° and 80°, for instance 70°.
  • the nozzles 16 In order to limit at most the risk of damaging the refractory lining of the inner walls of the combustion chamber 4 by the flames generated by the oxygen jets coming out of the collectors 15 and at the same time to minimise the mechanical stresses to which the nozzles 16 are subjected, which cause a rapid wear thereof, the nozzles 16 have a tilt angle with respect to the walls 17 of the collectors 15 comprised between 90° and 10°, preferably 90° and 30°, for instance 45°.
  • the end 12 a of the first duct 12 has slots 21 for the passage of the gas flow comprising oxygen from the first duct 12 to the collectors 15 .
  • the total end area of the collectors 15 defined at such slots 21 is determined so as to be equal or greater than the passage area of the duct 12 .
  • the comburent gas flows through the duct 12 and the collectors 15 with substantial axial motion, as shown by the dashed flow line 19 in FIG. 3 , and feeds transversally with its entire flow rate all nozzles 16 .
  • the nozzles 16 are all fed by corresponding parallel streamtubes of the gaseous flow comprising oxygen having equal velocity, thus obtaining jets of uniform velocity and hence flames of equal length along the entire perimeter of the collectors 15 .
  • This feature is not only advantageous in that it allows the achievement of an optimal and complete combustion in the combustion chamber 4 , but above all because it does not cause significant pressure drop in the flow of the comburent gas during its passage from the duct 12 to the collectors 15 . Moreover, this feature permits to realise in the end portion of the collectors 15 an extremely effective capillary cooling thus achieving a long operating life for the burner and hence relevant savings in term of loss of production of synthesis gas, maintenance costs and energy consumption.
  • the comburent gas (that is cooler than the process gas) is maintained in contact (lap contact) in an uniform and continuous way with each part of the duct 12 and of the collectors 15 , thus ensuring—always—an optimal cooling of such parts.
  • FIG. 3 clearly shows that the flows of the reactant gases flow into the burner 6 with a substantially axial motion (flow lines 18 , 19 ).
  • the oxygen flow is only subjected to a very small diverging deviation with respect to the axis A of the duct 12 , thus minimizing the pressure drop.
  • the gaseous flow comprising oxygen advantageously flows perpendicular with respect to the end 15 a of the collectors 15 , uniformly distributing itself along the entire length of such end 15 a . In doing so, it is possible to obtain an effective constant cooling also in this zone of the burner, that—being in direct contact with the hot burnt gases circulating inside the combustion chamber 4 —is subjected to wear and thermal stresses to a greater extent.
  • the end 12 a of the first duct 12 has a truncated-conical (upside down) shape in order to promote the passage of the gas flow comprising oxygen from the duct 12 to the collectors 15 , reducing at most possible pressure drops.
  • the end 12 a of the first duct 12 comprises inside it means for deviating the gas flow comprising oxygen toward the collectors 15 .
  • such means comprises a conical-shaped deflector 22 whose vertex is foreseen near an upper portion of the end 12 a of the first duct 12 .
  • the pressure drops of the gas flow comprising oxygen flowing in the first duct 12 may be further reduced providing a semicircular shape for the vertex 23 of the conical-shaped deflector 22 .
  • a seal collar is indicated with 24 , which is provided between the perforated baffle plates 20 and the duct 13 , for minimising the direct passage of the process gas from the hollow space 14 to the combustion chamber 4 .
  • this process is distinguished by the fact of comprising the steps of feeding the gas flow comprising oxygen (flow line 19 ) in the combustion chamber 4 in the form of a plurality of jets not laid the one upon the other with respect to the direction of the flow comprising hydrocarbons (flow line 18 ) and generated by corresponding parallel streamtubes having equal velocity; splitting the plurality of jets within the gas flow comprising hydrocarbons in the combustion chamber 4 so as to mix the gas flow comprising oxygen with amounts of gas flow comprising hydrocarbons at local constant ratio.
  • the jets of the gas flow comprising oxygen may have a diameter at the outlet of the feeding duct of the burner 6 comprised between 2 and 30 mm, preferably between 2 and 25 mm, for instance 10 mm.
  • the burner 6 according to the present invention further allows to carrying out the combustion reaction in the combustion chamber 4 by making the reactant gases to flow trough the duct 12 and the hollow space 14 at particularly low velocities.
  • velocities comprised between 20–200 m/s, preferably 40–100 m/s, for instance 50, 60 m/s.
  • the pressure drop of the gaseous flows is reduced and therefore subsequent energy dissipation is avoided, decreasing the energy consumption.
  • an optimal mixing of the gaseous flows in the chamber 4 is also ensured.
  • the comburent gas coming out of the collectors 15 collides with the process gas flow in such a way that every single jet of oxygen entrains a same amount of process gas and, in case of transversal feed between the reactant gases, also an equal amount of burnt gases circulating inside the combustion chamber 4 .
  • an optimal mixing between the gases is obtained with flames equal to each other and having the same temperature and composition conditions, to full advantage of the combustion reaction.

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  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
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US09/913,314 1999-02-10 2000-02-10 Secondary reforming process and burner Expired - Lifetime US7048772B1 (en)

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US09/913,314 US7048772B1 (en) 1999-02-10 2000-02-10 Secondary reforming process and burner
PCT/IB2000/000145 WO2000047517A1 (en) 1999-02-10 2000-02-10 Secondary reforming process and burner

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US20070261304A1 (en) * 2003-11-06 2007-11-15 Casale Chemicals S.A. Catalytic Secondary Reforming Process and Reactor for Said Process
US20090018222A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas
US20090018371A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing alcohols from syngas
US20090014689A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US20090018372A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing alcohols from syngas
US20090018221A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US20090093555A1 (en) * 2007-07-09 2009-04-09 Range Fuels, Inc. Methods and apparatus for producing syngas
EP2662133A1 (de) * 2012-05-09 2013-11-13 Casale Chemicals S.A. Verfahren zum Umgestalten eines Sekundärreformators
US20140070143A1 (en) * 2011-05-10 2014-03-13 Lurgi Gmbh Process and reactor for producing synthesis gas
CN107213810A (zh) * 2016-03-22 2017-09-29 中国石油化工股份有限公司 氧气与可燃气体高效、安全混合的方法
EP2811228B1 (de) 2013-06-07 2019-08-07 Haldor Topsøe A/S Brenner

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JP4363002B2 (ja) * 2002-04-18 2009-11-11 日産自動車株式会社 燃料改質システムとその暖機装置
CN100341616C (zh) * 2003-06-23 2007-10-10 卡萨尔化学股份有限公司 二次重整设备
FR2914396A1 (fr) * 2007-03-30 2008-10-03 Inst Francais Du Petrole Nouveau four de vaporeformage utilisant des bruleurs poreux
RU2515326C1 (ru) * 2012-10-04 2014-05-10 Открытое акционерное общество "Центральное конструкторское бюро морской техники "Рубин" Способ конверсии дизельного топлива и конвертор для его осуществления
DE102015121037A1 (de) * 2015-12-03 2017-06-08 Thyssenkrupp Ag Vorrichtung zur Sauerstoffverteilung in einem Oxidationsreaktor, Oxidationsreaktor und Anlage mit einer solchen Vorrichtung und Betriebsverfahren
CN107213809B (zh) * 2016-03-22 2023-06-02 中国石油化工股份有限公司 氧气与可燃气体旋流混合的方法
CN112707430B (zh) * 2021-01-12 2022-11-08 江西理工大学 一种燃烧室和燃烧合成超细氧化镧粉体的方法
CN116717790A (zh) * 2023-05-31 2023-09-08 海南大学 一种氢气燃烧炉头
CN116603361B (zh) * 2023-07-21 2023-09-26 天津市英格环保科技有限公司 一种中药加工用废气处理装置

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Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20070261304A1 (en) * 2003-11-06 2007-11-15 Casale Chemicals S.A. Catalytic Secondary Reforming Process and Reactor for Said Process
US8747497B2 (en) * 2003-11-06 2014-06-10 Casale Chemicals Sa Catalytic secondary reforming process and reactor for said process
US8551198B2 (en) * 2003-11-06 2013-10-08 Casale Chemicals Sa Catalytic secondary reforming process and reactor for said process
US20100221157A1 (en) * 2003-11-06 2010-09-02 Casale Chemicals S.A. Catalytic secondary reforming process and reactor for said process
US20090018221A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US20090018372A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing alcohols from syngas
US20090093555A1 (en) * 2007-07-09 2009-04-09 Range Fuels, Inc. Methods and apparatus for producing syngas
US20090014689A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US8142530B2 (en) 2007-07-09 2012-03-27 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US8153027B2 (en) 2007-07-09 2012-04-10 Range Fuels, Inc. Methods for producing syngas
US20090018371A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing alcohols from syngas
US9227895B2 (en) 2007-07-09 2016-01-05 Albemarle Corporation Methods and apparatus for producing alcohols from syngas
US20090018222A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas
US20140070143A1 (en) * 2011-05-10 2014-03-13 Lurgi Gmbh Process and reactor for producing synthesis gas
US9561483B2 (en) * 2011-05-10 2017-02-07 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Process and reactor for producing synthesis gas
WO2013167560A1 (en) * 2012-05-09 2013-11-14 Casale Chemicals Sa A method for revamping a secondary reformer
EP2662133A1 (de) * 2012-05-09 2013-11-13 Casale Chemicals S.A. Verfahren zum Umgestalten eines Sekundärreformators
US9561484B2 (en) 2012-05-09 2017-02-07 Casale Sa Method for revamping a secondary reformer
EP2811228B1 (de) 2013-06-07 2019-08-07 Haldor Topsøe A/S Brenner
CN107213810A (zh) * 2016-03-22 2017-09-29 中国石油化工股份有限公司 氧气与可燃气体高效、安全混合的方法
CN107213810B (zh) * 2016-03-22 2023-06-27 中国石油化工股份有限公司 氧气与可燃气体高效、安全混合的方法

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MXPA01008109A (es) 2002-08-30
PL191629B1 (pl) 2006-06-30
BR0008048B1 (pt) 2009-08-11
ATE268734T1 (de) 2004-06-15
CA2361704C (en) 2009-12-15
CN1340027A (zh) 2002-03-13
UA59487C2 (uk) 2003-09-15
DE60011425T2 (de) 2005-06-09
WO2000047517A1 (en) 2000-08-17
ID30326A (id) 2001-11-22
HUP0200615A2 (en) 2002-06-29
EP1183209A1 (de) 2002-03-06
RU2235058C2 (ru) 2004-08-27
BR0008048A (pt) 2001-10-30
DE60011425D1 (de) 2004-07-15
NZ513255A (en) 2003-08-29
HUP0200615A3 (en) 2003-07-28
CA2361704A1 (en) 2000-08-17
CN1167607C (zh) 2004-09-22
TR200102318T2 (tr) 2002-01-21
AU2313800A (en) 2000-08-29
PL350136A1 (en) 2002-11-04
AU771003B2 (en) 2004-03-11
EP1183209B1 (de) 2004-06-09
ZA200106119B (en) 2002-10-25

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